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US8318101B2 - Oil-derived hydrocarbon converter having an integrated combustion installation comprising carbon dioxide capture - Google Patents

Oil-derived hydrocarbon converter having an integrated combustion installation comprising carbon dioxide capture Download PDF

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Publication number
US8318101B2
US8318101B2 US12/086,659 US8665906A US8318101B2 US 8318101 B2 US8318101 B2 US 8318101B2 US 8665906 A US8665906 A US 8665906A US 8318101 B2 US8318101 B2 US 8318101B2
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Prior art keywords
particles
conversion system
reactor
catalyser
reduction reactor
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Expired - Fee Related, expires
Application number
US12/086,659
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English (en)
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US20100104482A1 (en
Inventor
Jean-Xavier Morin
Corinne Beal
Silvestre Suraniti
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GE Vernova GmbH
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Alstom Technology AG
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Assigned to ALSTOM TECHNOLOGY LTD reassignment ALSTOM TECHNOLOGY LTD ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SURANITI, SILVESTRE, BEAL, CORINNE, MORIN, JEAN-XAVIER
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/90—Regeneration or reactivation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • C10G11/182—Regeneration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/01—Fluidised bed combustion apparatus in a fluidised bed of catalytic particles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/70—Catalyst aspects
    • C10G2300/708—Coking aspect, coke content and composition of deposits
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/80—Additives
    • C10G2300/805—Water
    • C10G2300/807—Steam
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C2900/00—Special features of, or arrangements for combustion apparatus using fluid fuels or solid fuels suspended in air; Combustion processes therefor
    • F23C2900/99008—Unmixed combustion, i.e. without direct mixing of oxygen gas and fuel, but using the oxygen from a metal oxide, e.g. FeO
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the invention relates to an oil-derived hydrocarbon converter coupled to an integrated combustion installation with a carbon dioxide trap.
  • Such an oil-derived hydrocarbon converter includes a hydrocarbon catalytic cracking baffle in the presence of catalyst particles in fluidized phase and which fractionated oil cuts are recovered by ballistic separation of the particles and these fractional oil cuts.
  • a hydrocarbon catalytic cracking baffle in the presence of catalyst particles in fluidized phase and which fractionated oil cuts are recovered by ballistic separation of the particles and these fractional oil cuts.
  • this first baffle is customarily associated a catalyst particle regenerator, on which coke is deposited within the cracking vessel. In this regenerator, the catalyst particles are regenerated by burning the coke and are then recycled towards the cracking baffle.
  • Carbon dioxide is a greenhouse-effect gas that should be reduced from emissions, bringing about a total or partial capture of this dioxide.
  • the carbon dioxide can be captured in a reactor by washing with a solvent, for example, monoethanolamine, which selectively solubilises the carbon dioxide.
  • a solvent for example, monoethanolamine
  • the solvent is then regenerated by extracting the carbon dioxide due to heating by injecting steam in another reactor then the regenerated solvent is returned to the scrubber unit.
  • this solution has to be treated with nitrogen, which is also evacuated in part with the carbon dioxide at the top of the catalyst regenerator, which means proportioning the carbon dioxide trap in proportion with the quantity of nitrogen present.
  • the thermal regeneration entails the inconvenience of requiring large quantities of steam. This solution therefore consumes a lot of energy.
  • the oxygen is produced from air by using an air separation unit with a cryogenic system that consumes a lot of energy.
  • a carbonaceous solid combustion facility to include a reactor for reducing oxides, a first cyclone, an exchanger for flue gas heat recovery, a reactor for oxidizing oxides, a second cyclone, exchangers for controlling temperature of the circulating oxides, in which circulates an oxide which is reduced and then oxidized in each of both reactors.
  • the solid combustible material is milled before entering the oxide reduction reactor.
  • the oxides are reduced by first of all having them in contact with the fuel which reacts with the oxygen released by the oxide and then oxidized by contact with air which regenerates the oxide.
  • the reduced size of the solid fuel particles allows more complete and faster combustion and production of nearly 100% of fly ash.
  • This type of facility for combustion of carbonaceous solid materials operating at atmospheric pressure with integrated capture of carbon dioxide does not require any prior air separation. Because of the simplicity and the compactness of this system the costs of capturing carbon dioxide may be reduced while providing production of steam for generating electricity.
  • the invention proposes an integration of a system of this type to capture the carbon dioxide emitted in a hydrocarbon conversion facility such as specified above.
  • the carbon dioxide is captured, while providing the production of steam intended for the production of energy, and an optimal size and cost.
  • the invention proposes an oil-derived hydrocarbon conversion facility including a catalytic cracking baffle in the presence of catalyser particles in fluidized phase and a regenerator of the said catalyser particles by burning coke deposited on these, the said catalyst circulating between the said cracking vessel and said regenerator, the said regenerator being a reactor integrated in a combustion facility to produce steam including capturing the carbon dioxide, characterized in that the said regenerator is a reduction reactor for an oxygen support, supplied with solid fuel including the said particles supplied with coke and equipped with a separation cyclone for the solids and exchangers, this reduction reactor for the said oxygen support being associated with an oxidization reactor for the said oxygen support and equipped with a separation cyclone for the solids and exchangers, the said oxygen support circulating between these two reactors and in that the said oxygen support is constituted from metallic oxide particles of average diameter different from that of the aforesaid catalyser particles.
  • the said oxygen support can be constituted with the said catalyst particles.
  • the said oxygen support is formed from average diameter metallic oxide particles different from the said catalyst particles.
  • the said reduction reactor is a circulating fluidized bed fluidized by the steam and/or the recycled carbon dioxide and/or sulphur dioxide.
  • the installation includes in the cyclone outlet of the reduction reactor a siphon separating said metallic oxide particles directed towards the oxidization reactor and said catalyst particles directed towards the cracking baffle.
  • the said granulometric sorter has a circulating fluidized bed equipped with a separation cyclone.
  • said catalyst particles are re-introduced into the said cracking baffle by means of a rising duct of a defined height of which the load loss compensates the difference in pressure between the said baffle and the said granulometric sorter. This balances the difference in pressure between the circulation loop of the catalyst particles and the circulation loop of the metallic oxide particles.
  • the ratio between the average diameter of the metallic oxide particles and the catalyst particles is advantageously higher than 2:1.
  • Said metallic oxides can include iron oxide.
  • Said catalyst particles can consist of nickel oxide.
  • said solid fuel also includes oil residues, such as pitch, bitumen or asphalt, to generate sufficient power.
  • This diagram represents an installation conforming with the invention.
  • This installation includes an oil-derived hydrocarbon converter including a catalytic cracking baffle 1 in the presence of catalyst particles in a fluidized phase that is fed by a duct A 1 and a catalyst particle regenerator 2 by combusting the coke deposited on these, the catalyst circulating between the cracking baffle 1 and the regenerator 2 .
  • the catalyst particles are evacuated from the cracking baffle towards the regenerator by a supply duct 1 A and are re-injected from this regenerator towards the cracking baffle by a re-injection duct 2 A.
  • Some fractional oil cuts are obtained from the cracking baffle outlet by an outlet duct 1 B. In such a cracking baffle, the temperature is around 650° C. and the pressure about 2 bars.
  • the regenerator 2 is a reactor integrated in a combustion installation for producing steam with a carbon dioxide trap.
  • This regenerator 2 is a reduction reactor for an oxygen support, preferably formed from average diameter metallic oxide particles different from the catalyst particles, supplied in solid fuel including the particles provided from coke by the supply duct 1 A and equipped with a separation cyclone C 2 for the solids and exchangers E 2 .
  • the solid fuel fed by the duct A 2 can also include oil residues.
  • This reduction reactor is a heat source to the circulating fluidized bed fluidized with the steam by a supply duct 2 B and an air box 2 C introducing the fluidization steam in the lower part of the reduction reactor 2 .
  • This steam is mixed with the carbon dioxide or the sulphur dioxide recycled by an additional duct 2 D clearing in the same air box 2 C.
  • the temperature is around 900° C. and the pressure is atmospheric pressure.
  • the said reduction reactor 2 is a circulating fluidized bed fluidized by the steam and/or the recycled carbon dioxide and/or sulphur dioxide.
  • the cyclone C 2 In the top part of the reduction reactor 2 is installed the cyclone C 2 where the solid particles separated from the fly ash and the combustion gases containing carbon dioxide, sulphur dioxide and steam.
  • the fly ash and the combustion gases are brought to the heat exchangers E 2 and steam generators for the production of electricity.
  • the fly ash is separated from the combustion gases in a bag filter F 2 .
  • the combustion gases are then sent into a cooling and condensation circuit R 2 via a fan V 2 .
  • This circuit extracts water and the remaining H 2 SO 4 from the carbon dioxide which is then partially reintroduced into the reactor 2 by the additional duct 2 D.
  • the fly ash is separated from the metallic oxide particles by a granulometric separator S 2 to be stocked in a silo, whereas the metallic oxide particles are sent towards a silo 4 .
  • a second part coming from the cyclone is discharged towards a elimination device for the carbon residue 7 .
  • This elimination device 7 is fluidized by the steam from a steam inlet duct 8 , also supplying the feed duct 2 B of the reduction reactor 2 .
  • This fluidization separates the fine and light particles such as the carbon residual from the metallic oxide particles and reintroduces them into the reduction reactor 2 via a duct 7 A, while the denser and larger metallic oxide particles are transferred by a duct 7 B towards a second reactor 3 that is an oxidization reactor.
  • a composition example of such an elimination device 7 is described in the patent document FR 2 850 156.
  • the oxidization reactor 3 is equipped with a starting system D 3 that is supplied with fuel such as gas, a system of introducing the metallic oxide particles from the oxides silo 4 and a fluidization and oxidization system by a supply duct 9 .
  • This starting system D 3 reheats the reactors and the solids circulation loops up to a temperature threshold higher than 700° C. and starts the reactions.
  • the oxidization reactor 3 for the oxygen support containing metallic oxide particles of an average diameter different from the catalyst particles, is equipped with a separation cyclone for the solids C 3 and exchangers E 3 .
  • a bed composed of metallic oxides circulates in the oxidization reactor 3 that is fluidized by air coming from the inlet duct 9 supplying an air box 3 C.
  • the temperature is around 1000° C. and the pressure is atmospheric pressure.
  • the hot gases are cooled in the heat exchangers E 3 and steam generator for the production of electricity.
  • the oxide particles carried along are separated from the air by a bag filter F 3 and reintroduced into the oxide silo 4 , while an exhaust fan sends back air into the atmosphere via a chimney 10 .
  • the solid particles that have been extracted in the cyclone C 3 pass by to a siphon 11 from where a first part is transferred into the base of the reduction reactor 2 , a second part is re-circulated into the base of the oxidization reactor 3 and a third part is sent towards an outside bed 12 by air supplied by the air inlet duct 9 where a fluidized heat exchanger is situated, then finally reintroduced into the oxidization reactor 3 .
  • This exchanger controls the temperature in the oxidization reactor 3 .
  • Extra metallic oxide particles in the oxidization reactor 3 are possible from the oxide silo 4 via the duct 13 .
  • Extra oxide particles can be justified to compensate the losses by attrition in the different reactors 2 and 3 , so as to provide sufficient oxides to ensure the transfer of materials and the circulation of the solids.
  • the large ash particles or agglomerates are periodically extracted by an extraction duct 14 at the bottom of the oxidation reactor to a recovery silo.
  • the oxygen support is made up of metallic oxide particles different from the catalyst particles, which are, for example, made up from nickel oxide.
  • This metallic oxide preferably includes iron oxide and could also be manganese oxide, copper or nickel.
  • this oxygen support can be formed from the catalyst particles themselves.
  • the granulometric sorter 6 is not required.
  • the granulometry of these particles is chosen so that the ratio between the average diameter of the oxide particles and the catalyst particles is higher than 2:1.
  • the oxide particles have an average diameter of about 160 microns and the catalyst particles have an average diameter of about 60 microns.
  • the granulometric sorter 6 is formed from a circulating fluidized bed 6 A supplied in steam via the inlet duct 8 and equipped with a separation cyclone 6 B sized to carry out the sorting.
  • the evacuated oxide particles that are re-injected into the lower part of the reduction reactor 2 .
  • the catalyst particles are sent back into the cracking baffle 1 , by means of a rising duct 6 C of a defined height from which the load loss compensates the difference in pressure between the cracking baffle 1 and the granulometric sorter 6 . This transfer is done via a hopper 15 .
  • the oil-derived hydrocarbons and the catalyst particles are introduced into the cracking baffle 1 . Fractional oil cuts are obtained and the catalyst particles charged with coke and therefore carbon are evacuated in the reduction reactor 2 , possibly with oil residues.
  • This reduction reactor 2 being a circulating fluidized bed, an increased time delay in this reactor is obtained because of the internal circulation of the solids in this reactor and the recirculation via its cyclone C 2 .
  • the volatile materials clear very quickly after reheating the fuel and reacts with the oxygen cleared by the oxygen vehicle metallic oxide to perform a partial combustion that continues with the combustion of the fixed carbon, ensuring the elimination of coke carried by the catalyst particles that are regenerated on one hand, and on the other hand the reduction in possibly additional metallic oxide particles.
  • a part of the oxide bed is extracted at the bottom of the siphon 5 situated under the cyclone associated with this reduction reactor 2 , to be purified from the carbon residues that have not been transformed into fly ash, using the elimination device 7 that forms a barrier to the carbon in the installation, then reintroduced into the oxidization reactor 3 to be oxidized by the oxygen in the air.
  • Air weak in oxygen coming from the oxidization reactor 3 is cooled in the heat exchanger E 3 , that for practical purposes is formed from a plurality of exchangers, then any dust is removed in the bag filter F 3 and sent back out to the atmosphere.
  • the oxide particles regenerated after their passage into the oxidization reactor 3 are sent back towards the reduction reactor 2 to start a new cycle of transporting oxygen from the oxidization 3 reactor towards the reduction reactor 2 .
  • the quantity of oxides sent back into the reduction reactor 2 can be controlled by a flow control valve (not shown).
  • Another part of the oxide bed extracted with the siphon base 5 situated under the cyclone associated with the reduction reactor 2 is directed on the one hand downwards from the reduction reactor 2 to maintain a circulation of solids in the reactor 2 , and on the other hand towards the granulometric sorter 6 , that separates the regenerated catalyst particles that are re-injected into the cracking baffle 1 and the residual oxide particles which are reintroduced into the base of the reduction reactor.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Catalysts (AREA)
US12/086,659 2005-12-27 2006-12-22 Oil-derived hydrocarbon converter having an integrated combustion installation comprising carbon dioxide capture Expired - Fee Related US8318101B2 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR0554103 2005-12-27
FR0554103A FR2895413B1 (fr) 2005-12-27 2005-12-27 Installation de conversion d'hydrocarbures petroliers a installation de combustion integree comprenant une capture du dioxyde de carbone
PCT/FR2006/051415 WO2007074304A1 (fr) 2005-12-27 2006-12-22 Installation de conversion d'hydrocarbures petroliers a installation de combustion integree comprenant une capture du dioxyde de carbone

Publications (2)

Publication Number Publication Date
US20100104482A1 US20100104482A1 (en) 2010-04-29
US8318101B2 true US8318101B2 (en) 2012-11-27

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US (1) US8318101B2 (ru)
EP (1) EP1969092A1 (ru)
JP (1) JP4851538B2 (ru)
KR (1) KR100996373B1 (ru)
CN (1) CN101351530B (ru)
BR (1) BRPI0621263A2 (ru)
CA (1) CA2634129C (ru)
FR (1) FR2895413B1 (ru)
RU (1) RU2418843C2 (ru)
WO (1) WO2007074304A1 (ru)

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US9765961B2 (en) 2015-03-17 2017-09-19 Saudi Arabian Oil Company Chemical looping combustion process with multiple fuel reaction zones and gravity feed of oxidized particles
US10006632B2 (en) 2012-03-30 2018-06-26 General Electric Technology Gmbh Methods and apparatus for oxidation of unburnts

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US8007681B2 (en) * 2008-04-25 2011-08-30 Shell Oil Company Methods, compositions, and burner systems for reducing emissions of carbon dioxide gas into the atmosphere
FR2936301B1 (fr) * 2008-09-23 2010-09-10 Inst Francais Du Petrole Procede et dispositif optimises de combustion par boucle chimique sur des charges hydrocarbonees liquides
FR2937119B1 (fr) * 2008-10-15 2010-12-17 Air Liquide Procede de production d'energie et capture de co2
US20100281769A1 (en) * 2009-03-31 2010-11-11 Alstom Technology Ltd. Hot solids process selectively operable based on the type of application that is involved
ES2421210T3 (es) * 2009-06-12 2013-08-29 Alstom Technology Ltd Sistema para conversión de material combustible
JP5549130B2 (ja) * 2009-07-07 2014-07-16 株式会社Ｉｈｉ 二酸化炭素の回収方法及びその装置
FR2948177B1 (fr) * 2009-07-16 2011-08-05 Inst Francais Du Petrole Procede de combustion en boucle chimique avec controle independant de la circulation des solides
EP2567152A1 (en) * 2010-05-05 2013-03-13 Shell Oil Company Methods, compositions, and burner systems for reducing emissions of carbon dioxide gas into the atmosphere
FR2960941B1 (fr) * 2010-06-02 2014-11-14 Inst Francais Du Petrole Dispositif de separation de particules pour une boucle de combustion chimique
US9005431B2 (en) 2012-06-27 2015-04-14 Uop Llc Process and apparatus for distributing hydrocarbon feed to a catalyst stream
US8911673B2 (en) 2012-06-27 2014-12-16 Uop Llc Process and apparatus for distributing hydrocarbon feed to a catalyst stream
RU2496579C1 (ru) * 2012-10-18 2013-10-27 Федеральное государственное бюджетное учреждение науки Институт катализа им. Г.К. Борескова Сибирского отделения Российской академии наук Способ приготовления катализатора и способ каталитического сжигания топлив в псевдоожиженном слое
US9692069B2 (en) 2013-03-15 2017-06-27 Ziet, Llc Processes and systems for storing, distributing and dispatching energy on demand using and recycling carbon
US9550680B2 (en) 2013-06-21 2017-01-24 General Electric Technology Gmbh Chemical looping integration with a carbon dioxide gas purification unit
CN103486576A (zh) * 2013-09-25 2014-01-01 上海锅炉厂有限公司 一种三反应器结构的化学链燃烧装置和方法
CN103894239B (zh) * 2014-03-13 2016-09-14 张家港市天源机械制造有限公司 催化剂再生装置
JP5780333B2 (ja) * 2014-04-04 2015-09-16 株式会社Ihi 二酸化炭素の回収方法及びその装置
FR3022611B1 (fr) * 2014-06-19 2016-07-08 Ifp Energies Now Procede et installation de combustion par oxydo-reduction en boucle chimique avec un controle des echanges de chaleur
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UA118163C2 (uk) * 2015-08-14 2018-11-26 Оріон Інджинірд Карбонз Гмбх Способи і системи для видалення матеріалу частинок з потоку технологічних відпрацьованих газів
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CA2634129C (en) 2013-04-02
JP4851538B2 (ja) 2012-01-11
BRPI0621263A2 (pt) 2011-12-06
FR2895413A1 (fr) 2007-06-29
KR100996373B1 (ko) 2010-11-25
WO2007074304A1 (fr) 2007-07-05
FR2895413B1 (fr) 2011-07-29
RU2418843C2 (ru) 2011-05-20
JP2009521588A (ja) 2009-06-04
CN101351530A (zh) 2009-01-21
CA2634129A1 (en) 2007-07-05

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